JP2003002601A - Method and apparatus for manufacturing hydrogen gas - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a method and an apparatus for manufacturing hydrogen gas which can reduce cooling power for storage by utilizing coldness of a raw material when the hydrogen gas is manufactured from a liquefied natural gas and it is stored under a low temperature. SOLUTION: To use the apparatus for manufacturing hydrogen gas comprising a device 1 for boosting the pressure of the liquefied natural gas, a device 10 for generating hydrogen gas by using the liquefied natural gas as the reaction raw material, a device 20 for storing hydrogen gas under the low temperature, a heat exchanger 2, into which the above boosted liquefied natural gas and the above generate hydrogen gas are introduced and both gases are subjected to a heat exchange and from which the pre-cooled hydrogen gas is furnished to the device 20 for storing hydrogen gas, and an evaporator 4, in which the liquefied natural gas heated in the heat exchanger 2 is evaporated and from which at least a part of the evaporated gas is furnished to the device 10 for generating hydrogen gas.

Description

Detailed Description of the Invention

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hydrogen gas production method for producing hydrogen gas from liquefied natural gas as a raw material and then storing the hydrogen gas in a hydrogen storage device at a low temperature, and a production facility therefor.

[0002]

2. Description of the Related Art In recent years, the environmental destruction caused by energy consumption has become apparent, and the necessity of building a sustainable and sustainable society has come to be recognized. From this viewpoint, the use of hydrogen energy, which is a clean energy, is attracting attention, and it is expected to be used for automobile fuel, future aviation fuel and the like.

However, when hydrogen energy is used for various purposes, how to store hydrogen gas or the like becomes a problem from the viewpoint of volumetric efficiency. Hydrogen storage alloys have been conventionally known as a means for storing hydrogen gas.
Since the weight becomes a bottleneck, there is a difficulty in using it for transportation means such as an automobile, which has been an obstacle to practical use.

Therefore, in order to reduce the weight of the storage means,
Attention is focused on carbon-based hydrogen storage materials. One of them is activated carbon whose hydrogen adsorption capacity is enhanced by a special chemical activation method such as potassium hydroxide. When this is cooled to the temperature of liquefied natural gas or the temperature of liquefied nitrogen, it is possible to reduce the pressure and weight as compared with the mere high-pressure gas storage method. In addition, recently, attention has also been focused on the high adsorption capacity of hydrogen storage materials made of new materials such as carbon nanotubes.

On the other hand, finally, the production of hydrogen using natural energy is considered to be the ultimate form, but for the time being,
From the viewpoint of infrastructure development that uses hydrogen as a fuel for automobiles and the like, there is also interest in producing hydrogen from natural gas, which is relatively environmentally friendly. For example, as described in JP-A-8-92577 and the like, the hydrogen generation is performed by reacting methane, which is a main component of natural gas, with water to generate hydrogen and carbon monoxide, and further, carbon monoxide and water. A method is known in which hydrogen and carbon dioxide are generated by the reaction with and then hydrogen gas is purified by a separation membrane or a PSA (pressure swing adsorption) device.

[0006]

However, if the hydrogen gas produced by such a method is to be stored in the above-mentioned hydrogen storage material, a large amount of power is required for cooling the hydrogen gas, and the reduction thereof is required. Was wanted.

On the other hand, natural gas is liquefied for transportation from overseas and imported in the form of liquefied natural gas (LNG).
Although there are several examples of utilizing cold, most of them are simply vaporized by heat exchange with seawater and the like, and cold is not effectively used and is discarded.

Therefore, an object of the present invention is to produce a hydrogen gas from liquefied natural gas and store it at a low temperature by utilizing the cold of the raw material to reduce the cooling power for the storage. To provide a method for manufacturing hydrogen gas and a facility for manufacturing hydrogen gas.

[0009]

The above object can be achieved by the present invention as described below. That is, the step of boosting the liquefied natural gas, the step of introducing the boosted liquefied natural gas into a heat exchanger to heat itself by heat exchange, the step of vaporizing the heated liquefied natural gas, and the vaporized natural gas. Supplying at least a part of the gas as a reaction raw material to a hydrogen gas generator to generate hydrogen gas; and introducing the generated hydrogen gas into the heat exchanger to exchange heat with the liquefied natural gas to generate self gas. The method is characterized by including a step of pre-cooling to 50 ° C. or lower and a step of supplying pre-cooled hydrogen gas to a hydrogen storage device and storing it at a low temperature.

In the above, it is preferable that the generated hydrogen gas is pressurized by the auxiliary pressure boosting means and then introduced into the heat exchanger.

On the other hand, the hydrogen gas production equipment of the present invention stores a hydrogen gas at a low temperature, a booster for boosting liquefied natural gas, a hydrogen gas generator for producing hydrogen gas using natural gas as a reaction raw material. A hydrogen storage device, a heat exchanger that introduces the pressurized liquefied natural gas and the generated hydrogen gas to exchange heat between them, and supplies precooled hydrogen gas to the hydrogen storage device, and a heat exchanger therefor. And a means for supplying at least a part of the liquefied natural gas that has been heated and vaporized in step 1 to the hydrogen gas generator.

In the above, an auxiliary pressurizing means for pressurizing the hydrogen gas produced by the hydrogen gas producing device and then introducing it into the heat exchanger may be provided.

In the hydrogen storage device, a cold storage tank for storing a liquefied refrigerant for cooling the internal hydrogen storage unit and a refrigerant evaporative gas vaporized in the cold storage tank are heated by a heat exchanger,
After being compressed by a compressor and again introduced into the heat exchanger to be cooled, it is partially liquefied by expansion, and the gas is again introduced into the heat exchanger to recover refrigeration, and the liquefied liquefied refrigerant is again described above. It is preferable to provide a recycling route for supplying the cold storage tank.

Alternatively, in the hydrogen storage device, a cold storage tank for storing a liquefied refrigerant for cooling an internal hydrogen storage section, and a refrigerant evaporative gas vaporized in the cold storage tank are heated by a heat exchanger, and then a compressor is provided. After being compressed with and re-introduced into the heat exchanger to be cooled, it is partially liquefied by expansion, and the gas content is re-introduced into the heat exchanger to serve as a cold source, and the liquefied liquefied refrigerant is reintroduced into the cold storage tank. It is preferable to provide a recycle path for supplying and a path for introducing liquefied natural gas as another cold source in the heat exchanger of the recycle path.

[Operation and Effect] According to the manufacturing method of the present invention,
Since the liquefied natural gas as a raw material precools the produced hydrogen gas, the cooling power for hydrogen storage can be reduced by utilizing the refrigeration that has not been effectively used and has been discarded. Further, since the pressure of the liquefied natural gas is increased in the liquid state, the power can be reduced as compared with the case of separately compressing the gas raw material. As a result, when producing hydrogen gas from liquefied natural gas and storing it at a low temperature, it is possible to provide a method for producing hydrogen gas that can reduce the cooling power for storage by utilizing the cold of the raw material.

Further, when the generated hydrogen gas is pressurized by the auxiliary pressure boosting means and then introduced into the heat exchanger, it is possible to cope with the case where the hydrogen storage device requires high pressure.

On the other hand, according to the production facility of the present invention, due to the above-described effects, when hydrogen gas is produced from liquefied natural gas and stored at low temperature, the cold of the raw material is used for cooling for storage. Power can be reduced.

Further, when the auxiliary pressure increasing means for increasing the pressure of the hydrogen gas generated by the hydrogen gas generating device and then introducing the hydrogen gas into the heat exchanger is provided, it is possible to cope with the case where the hydrogen storage device requires high pressure.

When the hydrogen storage device includes the cold storage tank and the recycle path, the recycle path can generate a liquefied refrigerant that cools the hydrogen storage portion of the hydrogen storage device, and vaporizes the liquefied refrigerant in the cold storage tank. The latent heat can be used for efficient cooling.

When the hydrogen storage device is provided with the cold storage tank and the recycle path, and the heat exchanger of the recycle path is provided with a path for introducing liquefied natural gas as another cold source, the hydrogen storage apparatus is provided. Since the liquefied natural gas is also used as a cold source when generating the liquefied refrigerant that cools the hydrogen storage part, the cooling power can be further reduced.

[0021]

BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be described below with reference to the drawings.

The hydrogen gas production method of the present invention can be suitably carried out by the hydrogen gas production equipment of the present invention as shown in FIG. The production facility of the present invention comprises a booster 1 for boosting liquefied natural gas, a hydrogen gas generator 10 for producing hydrogen gas using natural gas as a reaction raw material, and a hydrogen storage device 20 for storing hydrogen gas at a low temperature. A heat exchanger 2 for introducing the pressurized liquefied natural gas and the generated hydrogen gas to exchange heat between them and supplying precooled hydrogen gas to the hydrogen storage device, and heating by the heat exchanger 2. A means for supplying at least a part of the vaporized liquefied natural gas to the hydrogen gas generator 10.

In this embodiment, two heat exchangers are provided,
Liquefied natural gas is introduced into the heat exchanger 2 for low temperature, most of it is vaporized by heating, and then the gas-liquid separator 5 separates gas and liquid, and the separated natural gas is heat-exchanged for high temperature. An example including an evaporator 4 that is introduced into the reactor 3 and that vaporizes the liquefied natural gas that is drawn out from the gas-liquid separator 5 and that supplies the hydrogen gas to the hydrogen gas generator 10 is shown.

In the present invention, the step of boosting the pressure of the liquefied natural gas is first performed, but it is preferable that the boosting is performed up to a pressure at which the boosting is not necessary in the subsequent step. Specifically, it is set according to the required pressure of the refining means of the hydrogen gas generator or the hydrogen storage device, and for example, when the hydrogen gas generator is equipped with the PSA purifying means, it is preferable to raise the pressure up to 10 to 40 barG. It is more preferred to carry out from 20 to 30 barG.
The liquefied natural gas used as the raw material is at about atmospheric pressure, about -1.
It is generally supplied at 55 ° C.

Then, the step of introducing the pressurized liquefied natural gas into the heat exchanger to heat itself by heat exchange is carried out.
In this embodiment, liquefied natural gas is introduced into the low temperature heat exchanger 2. Most of the vaporized liquefied natural gas is gas-liquid separated in the gas-liquid separator 5, and the gas phase component is introduced into the heat exchanger 3 for high temperature. That is, the heat exchanger 2 for low temperature performs the step of heating the liquefied natural gas and the step of vaporizing the liquefied natural gas.

On the other hand, in this embodiment, the liquefied natural gas derived from the liquid phase portion of the gas-liquid separator 5 is vaporized by the evaporator 4. Seawater, freon, or the like can be used as the heat medium of the evaporator 4, but cold heat (cold) generated by heat exchange can also be used as cooling water for the compressor or the like.

The natural gas supplied to the heat exchanger 3 is heated by exchanging heat with the produced hydrogen gas. The warmer 6 is provided when the temperature of the hydrogen gas discharged from the heat exchanger 3 is insufficient as the raw material temperature of the hydrogen gas generator 10. The heat medium is the same as that of the evaporator 4.

Next, the step of supplying the natural gas from the warmer 6 and the evaporator 4 as a reaction raw material to the hydrogen gas generator 10 to generate hydrogen gas is performed. The excess natural gas is supplied to another system via the valve 7. The hydrogen gas generator 10 may be any device as long as it can generate hydrogen gas using natural gas as a reaction raw material, and examples thereof include the following devices. Normally, such a hydrogen gas generator 10 requires a raw material compressor, but in the present invention, this can be omitted.

The hydrogen gas generator, as shown in FIG.
Desulfurization section 12 for desulfurizing natural gas, and steam reforming for producing high-concentration hydrogen-containing gas by adding water to desulfurized natural gas and then contacting this mixed fluid with a reforming catalyst for steam reforming. Section 13, raw material preheating section 11 for preheating the raw material supplied to the desulfurization section 12, preheating section 17 for preheating the mixed fluid supplied to the steam reforming section 13, and contacting the high-concentration hydrogen-containing gas with the shift conversion catalyst. A gas shift section 18 for producing a high-concentration hydrogen-containing gas having an increased hydrogen concentration, and a PSA section 19 for purifying a high-purity hydrogen gas by having an adsorbent for adsorbing and removing a reformed gas-containing component other than hydrogen. It is mainly composed of and.
In the present invention, TSA may be used instead of PSA.

The desulfurization section 12 is composed of an upstream hydrogenation catalyst layer which is internally filled with a hydrogenation catalyst and a downstream desulfurization agent layer which is filled with a desulfurization agent. In the hydrogenation catalyst layer, the raw material natural gas containing sulfur is brought into contact with the hydrogenation catalyst so that the sulfur content is hydrotreated to be reformed into hydrogen sulfide. Since these reactions are normally performed at 200 to 400 ° C., the raw material preheating unit 11 preheats the exhaust gas.

The steam reforming section 13 produces a high-concentration hydrogen-containing gas by bringing a gas obtained by adding steam to desulfurized natural gas into contact with a reforming catalyst to carry out steam reforming. The steam reforming section 13 is filled with a reforming catalyst in which an element such as platinum, ruthenium or nickel is carried on a carrier such as alumina or silica in a reaction tube.

The steam reforming (steam reforming) reaction for producing a gas having a high hydrogen content from a raw material natural gas includes a reforming reaction for producing hydrogen and carbon monoxide by a reaction between methane and water, and a carbon monoxide. It includes a carbon monoxide shift reaction that produces hydrogen and carbon dioxide by the reaction of water with water.

The steam reforming section 13 is housed on the burner 13a side of the steam reforming furnace. The steam reforming section 13 is heated to 650 to 850 ° C. by the heat of the burner 13a, and the above reforming reaction is performed. The main fuel of the burner 13a is PSA off-gas, and external air for combustion is supplied via an air pressure pump.

The gas shift section 18 converts the high-concentration hydrogen-containing gas discharged from the steam reforming section 13 into this gas shift section 18
By passing through the reformed gas cooler 14 on the upstream side, 20
After the temperature is lowered to 0 to 450 ° C., it is brought into contact with a shift catalyst to cause the carbon monoxide contained in the high-concentration hydrogen-containing gas to react with steam to convert into carbon dioxide and hydrogen, thereby removing carbon monoxide. Meanwhile, a high-concentration hydrogen-containing gas with a further increased hydrogen concentration is produced. As a shift catalyst,
Oxides such as iron-chromium and copper-zinc are used.

The PSA section 19 supplies the high-concentration hydrogen-containing gas discharged from the gas shift section 18 with a higher hydrogen concentration, to the shift gas cooler 15 upstream of the PSA section 19,
And 10 to 50 ° C. by passing through the gas-liquid separator 16,
A device for purifying high-purity hydrogen gas by adsorbing and removing reformed gas-containing components other than hydrogen (carbon monoxide, carbon dioxide, water, etc.) with an adsorbent after the temperature is lowered to 20 to 40 ° C. is preferable. The high-purity hydrogen gas purified by the PSA unit 19 is temporarily stored in the hydrogen holder 19a. On the other hand, the reformed gas-containing components other than hydrogen are once stored in an off-gas holder (not shown) and then supplied to the burner 13a as fuel. As this adsorbent,
Alumina, activated carbon, zeolite, etc. can be adopted.

Next, the produced hydrogen gas is introduced into the heat exchanger 2 to exchange heat with the liquefied natural gas to -50 ° C.
The step of precooling is performed below. However, in the present embodiment, prior to that, hydrogen gas is introduced into the heat exchanger 3 on the high temperature side to cool itself by heat exchange with the natural gas.

When the introduction pressure of hydrogen gas into the hydrogen storage device 20 is too low in relation to the operating pressure of the hydrogen storage device 20, the auxiliary boosting means 8 shown by the phantom line is set to the high temperature side. It may be provided on the inlet side of the heat exchanger 3.

Next, the step of supplying the precooled hydrogen gas to the hydrogen storage device 20 and storing it at a low temperature is performed. As the hydrogen storage device 20, for example, a device that adsorbs hydrogen gas at a temperature of −150 ° C. or lower and desorbs hydrogen gas under reduced pressure or under heating is preferable. As such a device, for example, there is a switching type hydrogen storage device 20 capable of simultaneously introducing and discharging hydrogen gas as shown in FIG. As shown in FIG. 3, the hydrogen storage device 20 includes cold storage tanks 21a and 21b having hydrogen storage units 22a and 22b therein.
And the heat exchanger 23. The heat exchanger 23 is provided to recover the cold of the refrigerant evaporative gas, but it may be omitted.

Liquefied refrigerants such as liquid nitrogen and liquefied natural gas supplied from the outside are stored in the internal spaces of the cold storage tanks 21a and 21b, and the refrigerant evaporative gas generated by the vaporization is discharged to the outside and exchanged with heat. Cold heat is recovered in the vessel 23. The liquefied refrigerant is passed through valves 27a and 27b to cool the tanks 21a and 21a.
b to the cold storage tank 21 via the valves 25a and 25b.
It is discharged from a and 21b. The discharged refrigerant evaporative gas is
It is cooled and liquefied by an independent refrigeration cycle (not shown) and is reused as a liquefied refrigerant.

The hydrogen storage parts 22a and 22b are filled with a hydrogen storage material such as activated carbon whose hydrogen adsorption capacity is enhanced by a special chemical activation method such as potassium hydroxide, so that the adsorption and desorption of hydrogen gas are uniform. It has a filling structure as is done. Further, the cold storage tanks 21a and 21b are provided with a vacuum heat insulating layer for insulating the outside.

In both of the hydrogen storage parts 22a and 22b, it is possible to carry out while switching the introduction and discharge of hydrogen gas. For example, while introducing hydrogen gas into the hydrogen storage unit 22a,
When the hydrogen gas is discharged from the hydrogen storage part 22b, the hydrogen gas is heat-exchanged with the refrigerant evaporative gas in the heat exchanger 23 to be pre-cooled and introduced into the hydrogen storage part 22a through the valve 24a, while the hydrogen storage part 22b is discharged. From valve 26b and exhaust port 2
Hydrogen gas is discharged via 8b.

Next, the conditions for introducing and discharging hydrogen gas in the hydrogen storage units 22a and 22b will be described. For example, the case where activated carbon is used as the hydrogen storage material of the hydrogen storage units 22a and 22b is as follows. The numerical values of the amount of adsorbed hydrogen gas and the like thereafter are R. Chahine and
P. Benard "ADSORPTION STORA
GE OF GASEOUS HYDROGEN AT
CRYOGENIC TEMPERATURES "Ad
vances in Cryogenic Engin
eering. Vol. 43 (1998), the numerical values read from the graph and the like are used.

The amount of hydrogen gas that can be adsorbed by activated carbon increases as the temperature decreases, and as the pressure difference between adsorption and desorption increases. When the desorption pressure is 1.4 bar, the amount of absorbed hydrogen gas per unit volume of activated carbon (total adsorption amount-remaining amount after desorption)
Is 15 at an adsorption pressure of 20 bar and a temperature of 77K.
It is 1.7 times that of 0K and about 10 times that of 273K. Therefore, it is preferable to use liquid nitrogen or the like as the liquid refrigerant in the cold storage tanks 21a and 21b to perform adsorption at -193 to -196 ° C.

Regarding the adsorption pressure, when the desorption pressure is 1.4 bar, the amount of stored hydrogen gas per unit volume of activated carbon is as shown in Table 1 at each adsorption pressure when the adsorption temperature is 77K. It becomes a value. Compared with the case of compressing and storing hydrogen gas, the adsorption method is particularly effective when the adsorption pressure is 5 to 60 bar. In the present invention, considering the discharge pressure of the hydrogen gas generator 10, etc., 20 -60 bar is preferred. The necessary boosting is achieved by the boosting device 1 and the auxiliary boosting means 8. The lower the desorption pressure, the better the occlusion efficiency.

[0045]

[Table 1] [Other Embodiments] Other embodiments of the present invention will be described below.

(1) In the above-described embodiment, an example is shown in which the refrigerant evaporative gas from the hydrogen storage device is cooled and liquefied by an independent refrigeration cycle to be reused as a liquefied refrigerant. As a recycling route, the refrigerant evaporative gas vaporized in the cold storage tank of the hydrogen storage device is heated by the heat exchanger, compressed by the compressor, introduced into the heat exchanger again, cooled, and then expanded by expansion. An example is a recycling route in which the partial liquefaction, the gas content is again introduced into the heat exchanger to recover cold, and the liquefied liquefied refrigerant is supplied again to the cold storage tank. At that time, the refrigerant partially liquefied due to expansion may be gas-liquid separated by a gas-liquid separator, or the refrigerant in a mixed phase state may be directly supplied to the cold insulation tank so that the cold insulation tank may have the function of gas-liquid separation. . In the present invention, as such a refrigerant,
Liquefied natural gas or liquid nitrogen can be used.

(2) On the other hand, from the viewpoint of more effectively utilizing the cooling of the liquefied natural gas as the raw material, the hydrogen storage device stores a liquefied refrigerant for cooling the internal hydrogen storage part, and a cold storage tank for storing the liquefied refrigerant. After liquefying the refrigerant evaporative gas vaporized in the cold storage tank, it is equipped with a recycle path for supplying again to the cold storage tank,
It is preferable that the heat exchanger in the recycling route is provided with a route for introducing liquefied natural gas as another cold source.
That is, it is preferable to use the cold of liquefied natural gas for reliquefaction of the refrigerant used for keeping the hydrogen storage device at a low temperature. As a recycling route at that time, the refrigerant evaporative gas vaporized in the cold storage tank is heated in the heat exchanger, compressed by the compressor, introduced into the heat exchanger again to be cooled, and then partially liquefied by expansion. Then, it is preferable that the gas is re-introduced into the heat exchanger to serve as a cold source, and the liquefied liquefied refrigerant is supplied again to the cold storage tank.

As a concrete recycling path, the apparatus shown in FIG. 4 or FIG. 5 in which the heat of the liquefied natural gas can be used also as the heat exchangers 2 and 3 and the introduction path of the liquefied natural gas are separately provided. There are some. The hydrogen storage device 20 shown in FIG. 3 is provided with the heat exchanger 23 for recovering the cold of the refrigerant evaporative gas, but when applied to the device shown in FIG. 4 or FIG. It can be omitted.

In the recycling path shown in FIG. 4, the refrigerant evaporative gas from the hydrogen storage device 20 is transferred to the heat exchangers 34, 33 ,.
2 and 3 are sequentially passed through to be cooled by heat exchange and compressed by the compressor 31 and the compressor 32, and then the heat exchangers 3, 2, 3
Cool through 3 sequentially. After that, the expansion valve (J-T
(Valve) 38 to flush and partially liquefy, and the partially liquefied refrigerant (for example, nitrogen) is gas-liquid separated by the gas-liquid separator 35. The gaseous refrigerant is again passed through the heat exchangers 33, 2 and 3 in sequence, heated by heat exchange, and supplied to the path between the compressor 31 and the compressor 32. The liquefied refrigerant is supplied to the hydrogen storage device 20 as a liquid refrigerant via the heat exchanger 34.

(3) Further, in the recycling path as shown in FIG. 5, the compressor 36 and the compressor 37 correspond to the compressor 31 and the compressor 32 in FIG. By using a compressor, it is possible to obtain the effect of reducing the capacity for reliquefaction of the refrigerant.

(4) In the above-described embodiment, an example is shown in which liquefied natural gas is introduced into a heat exchanger for low temperature and most of it is vaporized by heating, but it is heated to a temperature that does not vaporize. Alternatively, it may be heated or heated to a supercritical region. In the supercritical state, the natural gas derived from the heat exchanger on the low temperature side is introduced into the heat exchanger on the high temperature side while controlling the flow rate to maintain the thermal balance of heat exchange. You can

(5) In the above-described embodiment, an example in which the ortho-para conversion is not performed has been shown, but the heat exchanger 2 may have the function of the ortho-para conversion, for example. The ortho-para conversion can be performed by a known method using a catalyst.

(6) In the above-described embodiment, an example in which one booster is used to boost the pressure of liquefied natural gas has been described. However, there are two or more boosters and two or more routes thereafter,
The system other than the one system may be configured to be supplied to other devices outside the system or the power system. In that case, each system can be operated at different pressure, and one system can be operated at the same pressure as above,
Other systems may be set according to the required pressure of the supply destination.

Examples of the power supply to the power system include a method of supplying to a natural gas engine or a natural gas turbine for driving a compressor, a booster, an expansion turbine, etc., and to other devices outside the system. One example is the supply to the natural gas distribution line in the factory.

[Brief description of drawings]

FIG. 1 is a schematic configuration diagram showing an example of a hydrogen gas production facility of the present invention.

FIG. 2 is a schematic configuration diagram showing an example of a hydrogen gas generator according to the present invention.

FIG. 3 is a schematic configuration diagram showing an example of a hydrogen storage device according to the present invention.

FIG. 4 is a schematic configuration diagram showing an example of a refrigerating / recycling path of a hydrogen storage device according to the present invention.

FIG. 5 is a schematic configuration diagram showing another example of the refrigerating / recycling path of the hydrogen storage device according to the present invention.

[Explanation of symbols]

1 Booster 2 heat exchanger 4 evaporator 10 Hydrogen gas generator 19 PSA section 20 Hydrogen storage device 21a Cold storage tank 21b Cold storage tank 22a Hydrogen storage unit 22b Hydrogen storage unit

Claims (6)

[Claims] 1. A step of increasing the pressure of liquefied natural gas, a step of introducing the increased pressure of liquefied natural gas into a heat exchanger to heat itself by heat exchange, and a step of vaporizing the heated liquefied natural gas. By supplying at least a part of vaporized natural gas as a reaction raw material to a hydrogen gas generator to generate hydrogen gas, and introducing the generated hydrogen gas into the heat exchanger to exchange heat with the liquefied natural gas. A method for producing hydrogen gas, comprising: a step of precooling itself to −50 ° C. or lower; and a step of supplying precooled hydrogen gas to a hydrogen storage device and storing the hydrogen gas at a low temperature. 2. The method for producing hydrogen gas according to claim 1, wherein the generated hydrogen gas is boosted by an auxiliary booster before being introduced into the heat exchanger. 3. A pressure increasing device for increasing the pressure of liquefied natural gas,
A hydrogen gas generator for generating hydrogen gas using natural gas as a reaction raw material, a hydrogen storage device for storing hydrogen gas at a low temperature, a pressurized liquefied natural gas and the generated hydrogen gas are introduced to heat them. A heat exchanger for supplying hydrogen gas that has been exchanged and precooled to the hydrogen storage device; and a means for supplying at least a part of the liquefied natural gas heated and vaporized by the heat exchanger to the hydrogen gas generation device. Hydrogen gas production facility equipped with. 4. The facility for producing hydrogen gas according to claim 3, further comprising auxiliary boosting means for boosting the hydrogen gas generated by the hydrogen gas generator and introducing the boosted hydrogen gas into the heat exchanger. 5. The hydrogen storage device comprises a cold storage tank for storing a liquefied refrigerant for cooling an internal hydrogen storage unit, a refrigerant evaporative gas vaporized in the cold storage tank, heated by a heat exchanger, and then a compressor. After compressing with and introducing again into the heat exchanger to cool,
5. The hydrogen according to claim 3 or 4, further comprising a recycle path for partially liquefying by expansion, introducing a gas content into the heat exchanger again to recover refrigeration, and supplying the liquefied liquefied refrigerant to the cold storage tank again. Gas production equipment. 6. The hydrogen storage device comprises a cold storage tank for storing a liquefied refrigerant for cooling an internal hydrogen storage portion, and a refrigerant evaporative gas vaporized in the cold storage tank, heated by a heat exchanger, and then a compressor. After compressing with and introducing again into the heat exchanger to cool,
Partly liquefied by expansion, a gas component is again introduced into the heat exchanger as a cold source, and a liquefied liquefied refrigerant is provided again with a recycle path for supplying to the cold storage tank, and a heat exchanger for the recycle path is provided. The hydrogen gas production facility according to claim 3 or 4, further comprising a path for introducing liquefied natural gas as another cold source.